US10047320B2 - Method for recovering crude tall oil - Google Patents

Method for recovering crude tall oil Download PDF

Info

Publication number
US10047320B2
US10047320B2 US15/315,906 US201515315906A US10047320B2 US 10047320 B2 US10047320 B2 US 10047320B2 US 201515315906 A US201515315906 A US 201515315906A US 10047320 B2 US10047320 B2 US 10047320B2
Authority
US
United States
Prior art keywords
soap
acid
water
content
tall oil
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
US15/315,906
Other languages
English (en)
Other versions
US20170088794A1 (en
Inventor
Tiia Finer
Olli Timonen
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Stora Enso Oyj
Original Assignee
Stora Enso Oyj
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Stora Enso Oyj filed Critical Stora Enso Oyj
Assigned to STORA ENSO OYJ reassignment STORA ENSO OYJ ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: FINER, Tiia, TIMONEN, OLLI
Publication of US20170088794A1 publication Critical patent/US20170088794A1/en
Application granted granted Critical
Publication of US10047320B2 publication Critical patent/US10047320B2/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
    • C11B13/00—Recovery of fats, fatty oils or fatty acids from waste materials
    • C11B13/005—Recovery of fats, fatty oils or fatty acids from waste materials of residues of the fabrication of wood-cellulose (in particular tall-oil)
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
    • C11B13/00—Recovery of fats, fatty oils or fatty acids from waste materials
    • C11B13/02—Recovery of fats, fatty oils or fatty acids from waste materials from soap stock
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
    • C11B3/00—Refining fats or fatty oils
    • C11B3/006—Refining fats or fatty oils by extraction
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
    • C11B3/00—Refining fats or fatty oils
    • C11B3/02—Refining fats or fatty oils by chemical reaction
    • C11B3/04—Refining fats or fatty oils by chemical reaction with acids
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C11/00—Regeneration of pulp liquors or effluent waste waters
    • D21C11/0007—Recovery of by-products, i.e. compounds other than those necessary for pulping, for multiple uses or not otherwise provided for
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W30/00—Technologies for solid waste management
    • Y02W30/50—Reuse, recycling or recovery technologies
    • Y02W30/74—Recovery of fats, fatty oils, fatty acids or other fatty substances, e.g. lanolin or waxes

Definitions

  • This invention relates to a method for recovering crude tall oil from a soap.
  • black liquor is formed and removed from the produced pulp.
  • the removed black liquor comprises soap which needs to be separated from the black liquor since the soap comprises valuable raw materials.
  • Another reason to separate the soap from the black liquor is that the soap may cause problems during subsequent treatment steps of the black liquor.
  • the separated soap comprises crude tall oil (CTO), water, lignin, inorganic compounds and fibers.
  • CTO is a mixture of fatty and resin acids and unsaponifiables.
  • the fatty and resin acids of CTO are in the form of sodium salts in the soap.
  • the amount of each component in the soap depends on the raw material used during the pulping process and on the recovery process in which the soap is separated from the black liquor, i.e. the soap skimming process.
  • Crude tall oil is a valuable raw material and it is important to recover as much of the crude tall oil from the soap as possible. Crude tall oil can be used as a raw material for various chemicals and other products, e.g. biodiesel or detergents.
  • the amount of acid needed in order to separate the optimal amount of CTO from the soap depends on the quality of the soap, e.g. the CTO content, the water content, the fiber amount, the lignin content and/or the black liquor content.
  • It is an object of the present invention is to provide an improved method for recovering crude tall oil from a soap.
  • the present invention relates to a method for recovering crude tall oil from a soap wherein the method comprises the steps of:
  • the CTO recovery from a soap can be optimized by measuring the water content of the soap. It was found that there is a correlation between the water content and the CTO content of a soap. Consequently, by determining this correlation for a specific soap it is possible to measure the water content of the soap and then to know the CTO content of the soap. Furthermore, the amount of acid and water that needs to be added to the soap in order to separate the optimal amount of CTO depends on the amount of CTO presence in the soap.
  • the water content is measured on-line on a soap flow. It is thus possible to measure the water content on-line on a soap flow and then to directly regulate the added amount of acid and water.
  • the water content and the crude tall oil content in a soap flow tend to vary in a process and it is thus of importance to directly be able to regulate the needed amount of acid and water that is added to the soap in order to improve the recovery of the CTO.
  • the pH of the spent acid fraction of the acidulated soap after addition of the acid and water to the soap in step (d) is preferably less than 5, more preferably between 2-4,5 and even more preferably between 3-3,5.
  • the temperature of the acidulated soap in step (e) is preferably between 80 to 102° C., more preferably between 90 to 100° C. and even more preferably between 95 to 99° C.
  • the temperature of the acidulated soap is preferably regulated by addition by appropriate amount of steam in order to receive the optimal temperature.
  • step (e) is followed by a retention time before the soap is entered to the recovery step (f).
  • the retention time may be needed in order for the different phases of the soap to be clearly separated from each other and thus facilitate the recovery of the CTO.
  • the acid added in step (d) is a strong acid. It is preferred that the acid is sulfuric acid which is added in an amount of between 120 to 300 kg/t crude tall oil.
  • step (f) It may be preferred to use a hydrodynamic separator, centrifugal separator or decanter type process for the recovery of the separated crude tall oil in step (f).
  • the water content of said soap is preferably between 25 to 55 wt-%, preferably between 32 to 44 wt-% and even more preferably between 34-38 wt-%.
  • step (a) also comprises the step of measuring the black liquor content of the soap and adjusting the black liquor content to between 3 to 30 v-%. It has been found that it may be preferably to also measure the black liquor content of the soap since the needed amount of acid and water also may depend on the black liquor content of the soap.
  • This definition includes a soap that has been separated from a black liquor of an alkaline pulping process.
  • the definition includes all kind of soaps independent of the raw material used during the pulping process and the separation process of the soap from the black liquor.
  • This definition includes a soap of which the pH of the soap has changed from alkaline to acidic resulting in that the sodium salts of fatty and resin acids present in the soap are converted to acids.
  • This definition includes the amount of water presence in a soap, i.e. the water that is removed by evaporation.
  • the water content is calculated after measuring the dry content of the soap.
  • the dry content is measured as weigh percentage (wt-%) of the soap and it may be measured according to SCAN-N 22:77.
  • This definition includes the amount of crude tall oil, also called only tall oil, in a soap.
  • the crude tall oil (CTO) is measured as weight percentages (wt-%) of the soap and it may be measured according to the method PCTM 7 (Content of tall oil in tall oil soap, Pulp Chemicals Association, 1996) or by PCA-7.
  • This definition includes the acid concentration, which is measured as wt-% and calculated as follows:
  • This definition includes the total acid concentration, which is measured as wt-% and calculated as follows:
  • the quality of the soap may vary depending for example on the raw material used during the pulping process.
  • the water content and the crude tall oil content of the soap may vary due to the process parameters during the black liquor skimming, i.e. the parameters of the process in which the soap is separated from the black liquor.
  • the optimal amount i.e. the major part, of the CTO from the soap.
  • the present invention will improve the accuracy of the amount of acid and water that needs to be added to the soap. Too high amount and/or concentration of acid added will increase the risk of corrosion of the equipment and this will thus lead to an increased need for maintenance. Too low amount and/or concentration of acid added will not be able to separate the optimal amount of CTO from the acidulated soap, i.e. it will lead to CTO losses. Consequently, the present invention will lead to an improved CTO production with decreased amount of CTO losses to the reject fractions of the soap. Furthermore, the present invention also gives economically and environmentally benefits due to the improved control of the amount of acid that is added to the soap.
  • the present invention relates to a method for recovering crude tall oil from a soap wherein the method comprises the steps of: determining a correlation between the crude tall oil content and the water content of the soap, determining an amount of acid and water needed in order to separate an optimal amount of crude tall oil from the soap dependent on the crude tall oil content of the soap, measuring the water content of the soap, adding the optimal amount of acid and water to the soap based on the water content of the soap, mixing the added acid and water with the soap whereby an acidulated soap is formed and crude tall oil is separated and recovering the separated crude tall oil from the acidulated soap.
  • the correlation between the crude tall oil content and the water content needs to be determined for each specific soap.
  • the correlation is unique for each soap and it needs to be determined once for each soap quality. If the quality of the soap changes during the process, the correlation between the crude tall oil content and the water content needs to be determined again.
  • the quality can be changed if the raw material is changed, e.g. the type of wood used, during the pulping process or if other changes are made during the processes.
  • One way to know when the correlation needs to determined again, i.e. if the quality of the soap has changed too much is by measuring the yield of the separated CTO and compare it to the water content. If the amount of CTO separated and the amount of water added no longer correlates according to the determined correlation a new correlation needs to be determined.
  • the amount of acid and water needed for separation of the optimal amount of CTO at different CTO contents needs to be determined. This needs to be done once for each soap quality since the amount of acid and water needed may differ depending on the soap quality. In the same way, when the yield of the separated CTO is below acceptable levels, the optimal amount of added acid and water added needs to be re-determined.
  • the chemistry of a soap is complicated so it is not possible to theoretically calculate the amount of acid and water needed in order to separate the optimal amount of CTO.
  • both the sodium salts present in the soap as well as the black liquor of the soap will consume the added acid.
  • the amount of acid and water added to the soap in order to separate the optimal amount of CTO will depend on the CTO content of the soap.
  • the optimal amount acid and water needed also changes.
  • the amount of acid and water needed for a specific soap dependent on different CTO contents it is possible to know what amount of acid and water that needs to be added to the soap at a specific CTO content in order to separate the optimal amount of the CTO from the soap.
  • the water content is changed and the tall oil content of the soap for the different water contents is then determined. It would be preferred to determine the correlation within the typical range of the water content and tall oil content, e.g. with a water content of between 25-55 wt-% and a CTO content of between 40-70 wt-%.
  • sulphuric acid is used, suitable acid concentration is between 10 to 50 wt-%, preferably between 16 to 42 wt-%. It is important to minimize the evaporation of water during the separation in order to keep the acid concentration constant, i.e. if water is evaporated due to high temperature, the acid concentration will change.
  • the pH of the spent acid fraction of the acidulated soap after the addition of the acid and water is preferably below 5, preferably between 3-3,5.
  • the temperature of the acidulated soap during the determination of the acid and water is preferably between 80 to 102° C. It is preferred that the conditions, e.g. temperature and pH, and the acid used in step (b), i.e. during the determination of optimal amount of acid and water needed, are the same as in steps (d) and (e).
  • the separated CTO is thereafter recovered and the optimal amount of acid and water needed for the specific CTO content is seen since this amount provides the highest amount of recovered CTO. These tests will then be repeated for soaps with different CTO contents.
  • the acid and water as a mixture to the soap, i.e. in one step or stream as a diluted acid. It is also possible to add the acid and water in two separate steps or streams to the soap. It may also be possible to add a diluted acid, i.e. a mixture of acid and water, to the soap in one step or stream and to add water in a second step or stream. It may also be possible to first add water followed by addition of the acid. After the acid and water is added to the soap the acid, water and soap is mixed in order to make sure that a homogenous mixture, i.e. a well-mixed acidulated soap is formed. The time for the mixture depends on the amount of soap, acid and water added and also the mixing equipment used. All kinds of suitable mixing equipments may be used.
  • the acid is added to the soap in order for the sodium salts present in the soap to form acids which will have a different density compared to the other two phases of the soap, i.e. the lignin phase and the spent acid phase.
  • the addition of acid to the soap will form an acidulated soap.
  • the difference in density will enable the separation in three phases from each other.
  • the water is added to the soap in order to achieve the best density difference and thus achieve the optimal separation of the CTO from the soap.
  • the correlation between the CTO and the water content of the soap is determined and the amount of acid and water that needs to be added for different CTO contents is determined, it is possible to measure the water content of the soap and then to know the amount of acid and water that needs to be added to the soap in order to separate the optimal amount, i.e. the major part, of the CTO from the soap.
  • the amount of acid and water may be added continuously to the soap flow.
  • the water content is measured on-line on a soap flow.
  • the water content is preferably measured by the use of Near Infrared (NIR) spectroscopy, a refractometer, conductivity measurements or by any other known method.
  • NIR Near Infrared
  • the acid added in step (d) is a strong acid. It is preferred that the acid is sulfuric acid which is added in an amount of between 120 to 300 kg/t CTO, more preferably between 150-260 kg/t CTO and even more preferably between 160-220 kg/t CTO. These values are given as 100% sulphuric acid per ton of CTO contained in the soap. The amount of acid needed in order to separate the optimal amount of CTO depends on which acid that is used and must thus be measured separately for that specific acid.
  • the pH of the spent acid fraction of the acidulated soap in step (e), i.e. is preferably less than 5, more preferably between 2-4,5 and even more preferably between 3-3,5.
  • the temperature of the acidulated soap in step (e) is preferably between 80 to 102° C., more preferably between 90 to 100° C. and even more preferably between 95 to 99° C.
  • the temperature of the acidulated soap is preferably regulated by addition of the appropriate amount of steam in order to receive the optimal temperature of the soap.
  • the optimal temperature is the temperature at which the optimal amount of CTO is separated from the acidulated soap.
  • the temperature during the retention is also between 80 to 102° C., more preferably between 90 to 100° C. and even more preferably between 95 to 99° C.
  • the acid and water has been added and mixed with the soap an acidulated soap is formed and it is poured into the vessel in which the separation and recovery of the crude tall oil occurs.
  • the crude tall oil the lignin and the spent acid phases begin to separate from each other as a function of time.
  • the retention time is preferably between 1 second to 24 hours, more preferably between 1 second to 6 hours, more preferably between 1 second to 2 hours.
  • the time needed in order for the CTO phase to separate from the other phases depends on the separation method used, the process conditions during the step in which acid is added and on the soap quality e.g. the black liquor content of the soap.
  • the separation and the recovery of the CTO from the acidulated soap may be done in a hydrodynamic separator or decanter type process, however any known method can be used in order to separate the CTO. If the separation occurs in a hydrodynamic separator, the separation can be enhanced by addition of an internal spent acid flow in order to keep the lignin phase in movement in order to promote CTO separation.
  • the CTO phase is located on the top of the separator and overflows, and is thus removed and recovered, from the upper part of the separator.
  • the reject fraction, lignin and spent acid phases are removed from the separator from the middle respectively bottom part of the separator.
  • the black liquor content of the soap may also be possible to measure the black liquor content of the soap. If the water content is high and/or the black liquor content is high, it may be advantageous to concentrate the sample and reduce the black liquor content by any known method, e.g. by the use of a centrifugal method. This is due to the too high amounts of black liquor in the soap is not desirable since the black liquor will consume the added acid.
  • the black liquor content of the soap is between 3 to 30 volume %, even more preferably between 5 to 25 volume %. It may be possible to measure the black liquor content or other components of the soap, such as fatty acid resins, fibre composition etc. by Near Infrared (NIR) spectroscopy, by RAMAN spectroscopy or any other known method.
  • NIR Near Infrared
  • Suitable equipment for CTO recovery measurement should be similar to the equipment used in recovery processes used today, such as a decanter.
  • the CTO recovery is given as percentage of the present CTO content of the soap. It can be also be measured volumetrically and can be calculated as CTO recovered (kg)/(soap amount fed to the system (kg) ⁇ CTO content in the soap (wt-%)).
  • additives may be added before, together and/or after the addition of the acid and water to the soap.
  • FIG. 1 Shows the correlation between the soap density and the CTO content of the soap at 25° C.
  • FIG. 2 Shows the correlation between the soap density and the black liquor content of the soap at 25° C.
  • FIG. 3 Shows the correlation between the dry content and the CTO content of the soap at 25° C.
  • FIG. 4 Shows the correlation between the dry content and the black liquor content of the soap at 25° C.
  • FIG. 5 Shows the amount of separated CTO when the end pH of the spent acid is changed by charging different acid amounts to the soap.
  • FIG. 6 Shows the amount of separated CTO at different total acid concentrations when the end pH of the spent acid is constant.
  • FIG. 7 Shows the CTO separation rate depending on the water content of the soap.
  • FIG. 8 Shows the CTO recovery when the optimal amount of acid has been added.
  • FIG. 9 Shows the CTO recovery when a non-optimal amount of acid and water has been added.
  • the soap samples used in the experimental part as shown in FIGS. 1, 2, 3 and 4 were collected between June and July 2011 and the soap sample showed in FIGS. 5 and 6 was collected in June 2013 and the soap sample showed in FIG. 7 was collected in November 2013. All samples were collected from a soap acidulation process at a kraft pulp mill directly before the soap acidulation.
  • the origin of the soap used in FIGS. 1, 2, 3 and 4 was from a kraft pulping process using approximately 60% birch and 40% softwood (mainly pine). Fatty acid content was 44 m-%, resin acid content was 24 m-% (GC composition).
  • the origin of the soap used in FIGS. 5, 6 and 7 was also from a kraft pulping process using approximately 60% birch and 40% softwood (mainly pine).
  • the dry content of the soap was measured using the method SCAN-N 22:77 and the water content was calculated as described in the definition above for all the samples of FIGS. 1, 2, 3, 4, 5, 6 and 7 .
  • the black liquor content in the soap was measured by centrifugation (based on method of an accredited laboratory).
  • the CTO content in soap of FIGS. 3, 4, 5 and 6 has been measured by method PCTM7 (Pulp Chemicals Association, 1996).
  • the CTO content of the soap samples for FIG. 7 was analyzed using PCA-7.
  • the black liquor content in soap does not correlate linear with the measured soap density as illustrated in FIG. 1 .
  • soap density does also not correlate linearly with the CTO content in soap as shown in FIG. 2 .
  • FIG. 3 shows the correlation between the dry content of the soap and the CTO content of the soap at 25° C.
  • FIG. 4 shows the correlation between the dry content of soap and the black liquor content in soap at 25° C.
  • Both correlation lines are soap and/or mill specific and depend on the soap composition of the specific soap.
  • the soap dry content correlates linearly with the CTO content in the soap as well as with the black liquor content of soap as can be seen in FIGS. 3 and 4 . Consequently, once the correlation line is determined it is possible to measure the water content of the soap and then to know the CTO content and the black liquor content of the soap.
  • the amount of crude tall oil that is separated and recovered from the soap depends on the amount of acid added during the acidulation step. This can be seen in FIG. 5 .
  • the amount of crude tall oil that is separated and recovered from the soap depends on the acid concentration, i.e. the amount of water added during the acidulation step. This can be seen from FIG. 6 .
  • FIGS. 8 and 9 show an illustrative example of what happens when the water content of a soap changes but the amount of acid and water added to the soap is unchanged.
  • the water content of the soap shown in FIG. 8 is 35 wt-% and the water content of the soap shown in FIG. 9 is 45 wt-%.
  • the optimal amount of the CTO of the soap is separated and recovered, i.e. the amount of acid and water added to the soap with a water content of 35 wt-% is thus optimal.
  • the present CTO is separated and recovered. Consequently, it is very important to monitor the water content of the soap in order to be able to separate all CTO present in the soap.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Wood Science & Technology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Microbiology (AREA)
  • General Chemical & Material Sciences (AREA)
  • Detergent Compositions (AREA)
  • Fats And Perfumes (AREA)
  • Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)
US15/315,906 2014-06-05 2015-06-02 Method for recovering crude tall oil Active US10047320B2 (en)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
SE1450683A SE1450683A1 (sv) 2014-06-05 2014-06-05 Förfarande för utvinning av råtallolja
SE1450683 2014-06-05
SE1450683-6 2014-06-05
PCT/IB2015/054170 WO2015186060A1 (en) 2014-06-05 2015-06-02 Method for recovering crude tall oil

Publications (2)

Publication Number Publication Date
US20170088794A1 US20170088794A1 (en) 2017-03-30
US10047320B2 true US10047320B2 (en) 2018-08-14

Family

ID=54766233

Family Applications (1)

Application Number Title Priority Date Filing Date
US15/315,906 Active US10047320B2 (en) 2014-06-05 2015-06-02 Method for recovering crude tall oil

Country Status (10)

Country Link
US (1) US10047320B2 (zh)
EP (1) EP3152285B1 (zh)
CN (1) CN106459832B (zh)
BR (1) BR112016028447A2 (zh)
CA (1) CA2950870A1 (zh)
CL (1) CL2016003134A1 (zh)
PL (1) PL3152285T3 (zh)
RU (1) RU2698665C2 (zh)
SE (1) SE1450683A1 (zh)
WO (1) WO2015186060A1 (zh)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FI126505B (en) * 2015-07-08 2017-01-13 Upm Kymmene Corp Procedure and system for reducing residual soap in crude pine oil
US11034914B2 (en) * 2018-05-01 2021-06-15 Kraton Polymers Llc Desulfurized black liquor soap compositions and processes for producing

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3014879A (en) 1957-12-12 1961-12-26 Separator Ab Method of improving separability of products
US3404063A (en) * 1964-12-28 1968-10-01 Owens Illinois Inc By-product recovery from kraft black liquor
US3575952A (en) 1969-10-02 1971-04-20 Scm Corp Tall oil recovery
WO1993023132A2 (en) 1992-05-20 1993-11-25 Union Camp Corporation Improved acidification of tall oil soap using carbon dioxide
US5283319A (en) 1993-06-23 1994-02-01 Union Camp Corporation Process and control strategy for the recovery and use of excess carbon dioxide discharge from a high pressure carbon dioxide acidulation process
WO1996034932A1 (en) 1995-05-05 1996-11-07 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Neutralization of tall oil soap
EP1870445A1 (en) 2006-06-21 2007-12-26 Linde Aktiengesellschaft Process for producing tall oil and use of heating in the production of tall oil
CL2013000413A1 (es) 2010-09-10 2013-08-30 Arizona Chemical Co Llc Procedimiento para producir un aceite de resina bruto a partir de jabon de lejia negra a la vez que se retiran calcio y los lignatos que comprende combinar un jabon de lejia negra con un medio de lavado alcalino; y aceite de resina bruto.
WO2013173077A2 (en) 2012-05-14 2013-11-21 Arizona Chemical Company, Llc Semi-continuous acidulation process

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SU707526A3 (ru) * 1974-06-28 1979-12-30 Byarne Kholmbom Способ очистки мыла растительного происхождени
US7504478B2 (en) * 2007-01-26 2009-03-17 Nalco Company Additives for increasing the separation yield of tall oil soap from black liquors

Patent Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3014879A (en) 1957-12-12 1961-12-26 Separator Ab Method of improving separability of products
US3404063A (en) * 1964-12-28 1968-10-01 Owens Illinois Inc By-product recovery from kraft black liquor
US3575952A (en) 1969-10-02 1971-04-20 Scm Corp Tall oil recovery
WO1993023132A2 (en) 1992-05-20 1993-11-25 Union Camp Corporation Improved acidification of tall oil soap using carbon dioxide
US5283319A (en) 1993-06-23 1994-02-01 Union Camp Corporation Process and control strategy for the recovery and use of excess carbon dioxide discharge from a high pressure carbon dioxide acidulation process
WO1996034932A1 (en) 1995-05-05 1996-11-07 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Neutralization of tall oil soap
US5898065A (en) * 1995-05-05 1999-04-27 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Neutralization of tall oil soap
EP1870445A1 (en) 2006-06-21 2007-12-26 Linde Aktiengesellschaft Process for producing tall oil and use of heating in the production of tall oil
CL2013000413A1 (es) 2010-09-10 2013-08-30 Arizona Chemical Co Llc Procedimiento para producir un aceite de resina bruto a partir de jabon de lejia negra a la vez que se retiran calcio y los lignatos que comprende combinar un jabon de lejia negra con un medio de lavado alcalino; y aceite de resina bruto.
WO2013173077A2 (en) 2012-05-14 2013-11-21 Arizona Chemical Company, Llc Semi-continuous acidulation process
CL2014003077A1 (es) 2012-05-14 2015-07-03 Arizona Chemical Co Llc Proceso semicontinuo de acidulacion para la conversion de jabon de aceite alto en aceite alto crudo.

Non-Patent Citations (4)

* Cited by examiner, † Cited by third party
Title
Chilean Search Report for corresponding Chilean patent application, dated Nov. 24, 2017.
European Search Report for Corresponding European Patent Application, dated Dec. 21, 2017.
International Search Report for PCT/IB2015/054170, dated Sep. 23, 2015.
V.C. Uloth, Use of the Sodium Sesquisulphate By-Product of Chlorine Dioxide Generation for Tall Oil Soap Acidulation, Journal of Pulp and Paper Science: vol. 17, No. 6, Nov. 1991.

Also Published As

Publication number Publication date
WO2015186060A1 (en) 2015-12-10
CN106459832B (zh) 2020-02-14
EP3152285A1 (en) 2017-04-12
PL3152285T3 (pl) 2020-03-31
CL2016003134A1 (es) 2017-06-16
EP3152285A4 (en) 2018-01-24
RU2016150517A (ru) 2018-07-13
BR112016028447A2 (pt) 2017-08-22
US20170088794A1 (en) 2017-03-30
RU2016150517A3 (zh) 2019-01-15
CA2950870A1 (en) 2015-12-10
CN106459832A (zh) 2017-02-22
EP3152285B1 (en) 2019-08-07
RU2698665C2 (ru) 2019-08-28
SE1450683A1 (sv) 2015-12-06

Similar Documents

Publication Publication Date Title
US10047320B2 (en) Method for recovering crude tall oil
US8449764B2 (en) Method for using native bitumen markers to improve solvent-assisted bitumen extraction
Zhu et al. Equilibrium of lignin precipitation
RU2014145760A (ru) Способ автоматического определения содержания липких включений в процессе вторичной переработки волокон
CN101466890A (zh) 制备纤维材料的方法
SE454186B (sv) Sett for framstellning av kemimekanisk massa
Maquirriain et al. Crude glycerine characterization: analysis of free fatty acids, fatty acid methyl esters, and acylglycerides
Bogin Analysis of Binary Mixtures
US20090227767A1 (en) Process for producing tall oil and use of heating in the production of tall oil
CN102268832A (zh) 使用落叶松化机浆生产中高档文化用纸的制浆造纸工艺
US4462892A (en) Control of process aid used in hot water process for extraction of bitumen from tar sand
Wulfhorst et al. Compositional analysis of pretreated (beech) wood using differential scanning calorimetry and multivariate data analysis
SE450899B (sv) Forfarande for framstellning av kemisk massa enligt den sura sulfituppslutningsprocessen
Sullivan Continuous acidulation process for tall oil production
FI129928B (en) Method and arrangement for feedback-based control in chemical wood processing
Skvaril et al. Multivariate analysis models for wood properties combined with Open Modelica model for process performance monitoring
US5565134A (en) Method for enriching rosin acids from a hardwood-containing sulfate soap
CN110574956A (zh) 一种造纸法再造烟叶浆料质量稳定性的表征方法
Khakimova et al. Pulp depitching in the bisulfite pulping step
RU2029782C1 (ru) Способ получения таллового масла
WO2016120531A1 (en) Monitoring the chemical load of wastewater in an industrial process
WO2015007601A1 (en) Continuous process for the production of a valuable compound from lignocellulosic biomass
SE528094C2 (sv) Förfarande för separering av tvål från svartlut med tillsats av en neutral kolloidsubstans
Tran Soap separation efficiency at Gruvön mill: An evaluation of the process before and after a modification
Zampini et al. Potential benefit for production management of a pulp and paper company from using an ft-nir analyzer

Legal Events

Date Code Title Description
AS Assignment

Owner name: STORA ENSO OYJ, FINLAND

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:FINER, TIIA;TIMONEN, OLLI;REEL/FRAME:040736/0787

Effective date: 20161118

STCF Information on status: patent grant

Free format text: PATENTED CASE

CC Certificate of correction
MAFP Maintenance fee payment

Free format text: PAYMENT OF MAINTENANCE FEE, 4TH YEAR, LARGE ENTITY (ORIGINAL EVENT CODE: M1551); ENTITY STATUS OF PATENT OWNER: LARGE ENTITY

Year of fee payment: 4